Bio-based synthetic  fluids

ABSTRACT

A method is provided involving altering the viscosity of bio-derived paraffins to produce a paraffinic fluid, where the altering step includes chlorinating the bio-derived paraffins; the bio-derived paraffins include a hydrodeoxygenated product produced by hydrodeoxygenating a bio-based feed where the bio-based feed includes bio-derived fatty acids, fatty acid esters, or a combination thereof; the bio-derived paraffins include n-paraffins; and the n-paraffins have a biodegradability of at least 40% after about 23 days of exposure to microorganisms. Also provided are methods of protecting and/or cleaning a substance by applying the paraffinic fluid.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a divisional of U.S. application Ser. No. 13/871,972, filed Apr. 26, 2013, which claims the benefit of priority from U.S. Provisional Application No. 61/809,183, filed on Apr. 5, 2013, each of which is incorporated herein by reference in its entirety for any and all purposes.

FIELD

The technology relates to production of synthetic fluids from bio-derived feeds. More particularly, this technology relates to methods for conversion of animal fat, vegetable oils, and other sources of bio-based fatty acid/esters into paraffinic fluids suitable for use as solvents, industrial process fluids, and lubricating base oils.

BACKGROUND

Low aromatic hydrocarbon fluids, i.e. typically containing less than 1 wt % total aromatics, are used in a diverse range of applications where chemical inertness, thermal/oxidative stability, low toxicity, and low odor are desired. These hydrocarbons are characterized by their paraffinic nature, a carbon number distribution in the C₅-C₄₀ range, preferably in the C₁₅-C₄₀ range. For most applications, the preferred fluids have a flash point greater than about 100° C. Other properties specified for hydrocarbon fluids include viscosity (specification range dictated by application), and pour point (typically <−10° C.). Mineral oil is an example of a low aromatic hydrocarbon fluid.

As a result of a number of industry trends, such as increased demand for drilling and hydraulic fracturing fluids and tightening environmental standards concerning eco-toxicity, biodegradability, and work place safety/health, demand for such paraffinic fluids has experienced rapid growth. This has coincided with an increased demand for middle distillate fuels (C₁₀-C₂₀ hydrocarbons) that compete for much of the same petroleum molecules. Furthermore, with high aromatic feeds such as tar sands finding their way into the North American petroleum pool, more extensive upgrading (such as aromatic hydrogenation) is required in order to meet fluid product specifications. Use of mineral oils in cosmetics and food preparation is banned in the European Union due to concerns about presence of trace amounts of carcinogenic polyaromatic hydrocarbons—thus providing the need for synthetic products that are inherently free of these aromatic components.

Synthetic hydrocarbon products have been used for some industrial fluid applications. For example C₁₆/C₁₈ linear alpha olefins (LAOs) from oligomerization of ethylene, are used as drilling base fluids. However, this synthetic route is non-selective, producing a wide distribution of even carbon number LAOs, mostly in the C₄ to C₁₀ range, such that further expensive processing and separation steps are required to achieve the desired LAO product. Moreover, these even carbon number LAOs in the C₄ to C₁₀ range are chemical intermediates and not end-products suitable for use in industrial fluid applications.

Use of the Fischer-Tropsch process for producing synthetic hydrocarbons suitable for certain hydrocarbon fluid applications has also been reported. However, the FT process is very capital intensive and most of the FT manufacturing is dedicated to fuel production. Because the hydrocarbon range of interest for synthetic hydrocarbon fluids comprises a small percentage of the wide distribution of FT hydrocarbons (C1-C50+), it is more economical to hydrocrack and hydrotreat the FT wax and light oil fractions into complex compositions for fuel use.

There is thus a need for new processes for producing hydrocarbon fluids from alternative feeds. More specifically, there is a need for hydrocarbon fluid products that, based on their feedstocks and conversion processes, are substantially free of aromatics without further processing such as by aromatic hydrogenation conditions.

SUMMARY

In an aspect, a method is provided involving altering the viscosity of bio-derived paraffins to produce a paraffinic fluid, where the altering step includes oligomerizing bio-derived paraffins, unsaturating bio-derived paraffins, chlorinating bio-derived paraffins, or a combination of any two or more thereof; the bio-derived paraffins are produced by hydrodeoxygenating a bio-based feed; the bio-based feed comprises bio-derived fatty acids, fatty acid esters, or a combination thereof; the bio-derived paraffins comprise n-paraffins; and the n-paraffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least 40% after about 23 days of exposure to microorganisms.

In some embodiments, oligomerizing bio-derived paraffins includes contacting the bio-derived paraffins with an organic peroxide to produce an oligomerized product, where the oligomerized product has a kinematic viscosity of at least about 10 cSt at 40° C. In some embodiments, the oligomerized product has a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. In some embodiments, the oligomerized product is a dimer, trimer, tetramer, or a mixture of any two or more thereof. In some embodiments, the organic peroxide is present in an amount between about 2 wt % and about 40 wt % based on the total weight of paraffins and organic peroxide. In some embodiments, the organic peroxide comprises di-tert butyl peroxide (DTBP), 2,5-dimethyl 2,5-di(t-butylperoxy)hexane, dicumyl peroxide, dibenzoyl peroxide, dipropyl peroxide, ethyl propyl peroxide, or tert-butyl tert-amyl peroxide. In some embodiments, the contacting is performed at a temperature between about 50° C. and about 250° C. In some embodiments, the oligomerized product is used as a drilling fluid, a hydraulic fracturing fluid, a metal working fluid, a protecting agent, or a combination of any two or more thereof.

In some embodiments, chlorinating the bio-derived paraffins includes contacting the bio-derived paraffins with chlorine gas at a temperature between about 60° C. and about 150° C. to produce a chlorinated product, where the chlorinated product comprises haloalkanes; and the chlorinated product has a kinematic viscosity of greater than about 10 cSt at 40° C. In some embodiments, the chlorinated product is used as a protecting agent, a cleaning agent, or a combination of both. In some embodiments, the chlorinated product acts as a flame retardant. In some embodiments, the chlorinated product is used to clean fabric, metal, or plastic.

In some embodiments, unsaturating the bio-derived paraffins comprises dehydrogenation of the bio-derived paraffins by contacting the bio-derived paraffins with a dehydrogenation catalyst at a temperature from about 360° C. to about 660° C. to produce an olefinic fluid, where the olefinic fluid comprises at least about 10 wt % internal olefins in the C₁₅ to C₁₈ range; and the olefinic fluids have a kinematic viscosity of less than about 10 cSt at 40° C. In some embodiments, the olefinic fluid comprises at least about 20 wt % internal olefins in the C₁₅ to C₁₈ range. In some embodiments, the method further involves oligomerizing the olefinic fluid to produce dimers, trimers, tetramers, or a mixture of any two or more thereof. In some embodiments, the olefinic fluid is used as a hydraulic fracturing fluid, as a drilling fluid, or a combination of the two.

In some embodiments, the bio-derived paraffins are produced by hydrodeoxygenating the bio-based feed to produce a hydrodeoxygenated product; and at least partially hydroisomerizing the hydrodeoxygenated product to produce a hydroisomerized product; where the bio-derived paraffins comprise the hydrodeoxygenated product and the hydroisomerized product; the hydrodeoxygenated product comprises n-paraffins; the hydroisomerized product comprises isoparaffins where at least about 80 wt % of the isoparaffins are mono-methyl branched paraffins; the mono-methyl branched paraffins comprise less than about 30 wt % terminal branched isoparaffins; and the isoparaffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. In some embodiments, the hydrodeoxygenated product includes n-paraffins in the range of about 80 wt % to about 100 wt %; cycloparaffins in the range of about 1 wt % to about 10 wt %; and less than about 1 wt % total aromatics.

In some embodiments, the bio-derived fatty acids, fatty acid esters, or a combination thereof comprises algae oils, beef tallow, camelina oil, canola oil, rapeseed oil, castor oil, choice white grease, coconut oil, coffee bean oil, corn oil, cottonseed oil, fish oils, hemp oil, Jatropha oil, linseed oil, mustard oil, palm oil, palm kernel oil, poultry fat, soybean oil, sunflower oil, tall oil, tall oil fatty acid, Tung oil, used cooking oils, yellow grease, products of the food industry, or combinations of any two or more thereof. In some embodiments, the bio-derived fatty acids, fatty acid esters, or a combination thereof comprise soybean oil, corn oil, cottonseed oil, canola oil, coconut oil, sunflower oil, palm oil, palm kernel oil, rapeseed oil, or a combination of any two or more thereof.

In an aspect, a method is provided involving producing an orifice in a substrate by at least injecting a viscosity-altered paraffinic fluid into the substrate, wherein the paraffinic fluid includes a hydrodeoxygenated product and a hydroisomerized product; the hydrodeoxygenated product is produced by hydrodeoxygenating a bio-derived feed; the hydroisomerized product is produced by at least partially hydroisomerizing the hydrodeoxygenated product; the bio-derived feed includes bio-derived fatty acids, fatty acid esters, or a combination thereof; the hydrodeoxygenated product includes n-paraffins; the hydroisomerized product includes isoparaffins; the paraffinic fluid contains less than about 1 wt % aromatics; and the n-paraffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms; the isoparaffins are at least about 80 wt % mono-methyl branched paraffins where the mono-methyl branched paraffins comprise less than about 30 wt % terminal branched isoparaffins, have a kinematic viscosity of less than about 10 cSt at 40° C., and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. In some embodiments, the substrate includes a soil substrate, a topsoil substrate, a subsoil substrate, a clay substrate, a sand substrate, a rock substrate, or a stone substrate. In some embodiments, the step of producing an orifice includes hydraulic fracturing of the substrate with the paraffinic fluid.

In another aspect, a method is provided involving protecting a substance by applying a paraffinic fluid. In the method, the paraffinic fluid includes a hydrodeoxygenated product; where the hydrodeoxygenated product is produced by hydrodeoxygenating a bio-derived feed; the bio-derived feed comprises bio-derived fatty acids, fatty acid esters, or a combination thereof; the hydrodeoxygenated product comprises n-paraffins; the paraffinic fluid contains less than 1 wt % aromatics; and the n-paraffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least 40% after about 23 days of exposure to microorganisms. In some embodiments, the hydrodeoxygenated product includes n-paraffins in the range of about 80 wt % to about 100 wt %; cycloparaffins in the range of about 1 wt % to about 10 wt %; less than about 1 wt % total aromatics. In some embodiments, the paraffinic fluid further comprises a hydroisomerized product produced by at least partially hydroisomerizing the hydrodeoxygenated product; where the hydroisomerized product comprises isoparaffins where at least about 80 wt % of the isoparaffins are mono-methyl branched paraffins; the mono-methyl branched paraffins comprise less than about 30 wt % terminal branched isoparaffins; and the isoparaffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms.

In some embodiments, the substance is a food crop, a metal, or wood. In some embodiments, protecting involves solvating the substance. In such embodiments, the substance includes pesticides, herbicides, paints, inks, or coatings. In some embodiments, protecting involves cleaning the substance with the paraffinic fluid In such embodiments, the substance comprises fabric, metal, or plastic. In some embodiments, protecting involves lubricating the substance where the substance is metal.

In an aspect, a method is provided which involves producing an orifice in a substrate by at least injecting a paraffinic fluid into the substrate, wherein the paraffinic fluid comprises a hydrodeoxygenated product; the hydrodeoxygenated product is produced by hydrodeoxygenating a bio-derived feed; the bio-derived feed comprising bio-derived fatty acids, fatty acid esters, or a combination thereof; the hydrodeoxygenated product comprises n-paraffins; the paraffinic fluid contains less than about 1 wt % aromatics; and the n-paraffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. In some embodiments, the hydrodeoxygenated product includes n-paraffins in the range of about 80 wt % to about 100 wt %; cycloparaffins in the range of about 1 wt % to about 10 wt %; and less than about 1 wt % total aromatics. In some embodiments, the paraffinic fluid further includes a hydroisomerized product produced by at least partially hydroisomerizing the hydrodeoxygenated product; wherein the hydroisomerized product comprises isoparaffins where at least about 80 wt % of the isoparaffins are mono-methyl branched paraffins; the mono-methyl branched paraffins comprise less than about 30 wt % terminal branched isoparaffins; and the isoparaffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms.

In some embodiments, the substrate comprises a soil substrate, a topsoil substrate, a subsoil substrate, a clay substrate, a sand substrate, a rock substrate, or a stone substrate. In some embodiments, the bio-derived fatty acids, fatty acid esters, or a combination thereof comprises algae oils, beef tallow, camelina oil, canola oil, rapeseed oil, castor oil, choice white grease, coconut oil, coffee bean oil, corn oil, cottonseed oil, fish oils, hemp oil, Jatropha oil, linseed oil, mustard oil, palm oil, palm kernel oil, poultry fat, soybean oil, sunflower oil, tall oil, tall oil fatty acid, Tung oil, used cooking oils, yellow grease, products of the food industry, or combinations of any two or more thereof. In some embodiments, the bio-derived fatty acids, fatty acid esters, or a combination thereof comprise soybean oil, corn oil, cottonseed oil, canola oil, coconut oil, sunflower oil, palm oil, palm kernel oil, rapeseed oil, or a combination of any two or more thereof. In some embodiments, the step of producing an orifice comprises hydraulic fracturing of the substrate with the paraffinic fluid.

BRIEF DESCRIPTION OF THE DRAWING

FIG. 1 depicts a process for conversion of a bio-derived feed to industrial fluids, the process comprising hydrodeoxygenation, hydroisomerization, peroxide-initiated oligomerization, and fractionation

DETAILED DESCRIPTION

Various embodiments are described hereinafter. It should be noted that the specific embodiments are not intended as an exhaustive description or as a limitation to the broader aspects discussed herein. One aspect described in conjunction with a particular embodiment is not necessarily limited to that embodiment and can be practiced with any other embodiment(s).

As used herein, “about” will be understood by persons of ordinary skill in the art and will vary to some extent depending upon the context in which it is used. If there are uses of the term which are not clear to persons of ordinary skill in the art, given the context in which it is used, “about” will mean up to plus or minus 10% of the particular term.

The use of the terms “a” and “an” and “the” and similar referents in the context of describing the elements (especially in the context of the following claims) are to be construed to cover both the singular and the plural, unless otherwise indicated herein or clearly contradicted by context. Recitation of ranges of values herein are merely intended to serve as a shorthand method of referring individually to each separate value falling within the range, unless otherwise indicated herein, and each separate value is incorporated into the specification as if it were individually recited herein. All methods described herein can be performed in any suitable order unless otherwise indicated herein or otherwise clearly contradicted by context. The use of any and all examples, or exemplary language (e.g., “such as”) provided herein, is intended merely to better illuminate the embodiments and does not pose a limitation on the scope of the claims unless otherwise stated. No language in the specification should be construed as indicating any non-claimed element as essential.

In general, “substituted” refers to an alkyl or aryl group as defined below (e.g., an alkyl group) in which one or more bonds to a hydrogen atom contained therein are replaced by a bond to non-hydrogen or non-carbon atoms. Substituted groups also include groups in which one or more bonds to a carbon(s) or hydrogen(s) atom are replaced by one or more bonds, including double or triple bonds, to a heteroatom. Thus, a substituted group will be substituted with one or more substituents, unless otherwise specified. In some embodiments, a substituted group is substituted with 1, 2, 3, 4, 5, or 6 substituents. Examples of substituent groups include: halogens (i.e., F, Cl, Br, and I); hydroxyls; alkoxy, alkylperoxy, alkenoxy, alkynoxy, aryloxy, arylperoxy, aralkyloxy; carbonyls (oxo); carboxyls; esters; urethanes; oximes; hydroxylamines; alkoxyamines; aralkoxyamines; thiols; sulfides; sulfoxides; sulfones; sulfonyls; sulfonamides; amines; N-oxides; hydrazines; hydrazides; hydrazones; azides; amides; ureas; amidines; guanidines; enamines; imides; isocyanates; isothiocyanates; cyanates; thiocyanates; imines; nitro groups; nitriles (i.e., CN); and the like.

As used herein, “alkyl” groups include straight chain and branched alkyl groups having from 1 to about 20 carbon atoms, and typically from 1 to 12 carbons or, in some embodiments, from 1 to 8 carbon atoms. As employed herein, “alkyl groups” include cycloalkyl groups as defined below. Alkyl groups may be substituted or unsubstituted. Examples of straight chain alkyl groups include methyl, ethyl, n-propyl, n-butyl, n-pentyl, n-hexyl, n-heptyl, and n-octyl groups. Examples of branched alkyl groups include, but are not limited to, isopropyl, sec-butyl, t-butyl, neopentyl, and isopentyl groups. Representative substituted alkyl groups may be substituted one or more times with, for example, amino, thio, hydroxy, cyano (i.e. CN), alkoxy, and/or halo groups such as F, Cl, Br, and I groups.

Cycloalkyl groups are cyclic alkyl groups such as, but not limited to, cyclopropyl, cyclobutyl, cyclopentyl, cyclohexyl, cycloheptyl, and cyclooctyl groups. In some embodiments, the cycloalkyl group has 3 to 8 ring members, whereas in other embodiments the number of ring carbon atoms range from 3 to 5, 6, or 7. Cycloalkyl groups may be substituted or unsubstituted. Cycloalkyl groups further include polycyclic cycloalkyl groups such as, but not limited to, norbornyl, adamantyl, bornyl, camphenyl, isocamphenyl, and carenyl groups, and fused rings such as, but not limited to, decalinyl, and the like. Cycloalkyl groups also include rings that are substituted with straight or branched chain alkyl groups as defined above. Representative substituted cycloalkyl groups may be mono-substituted or substituted more than once, such as, but not limited to: 2,2-; 2,3-; 2,4-; 2,5-; or 2,6-disubstituted cyclohexyl groups or mono-, di-, or tri-substituted norbornyl or cycloheptyl groups, which may be substituted with, for example, alkyl, alkoxy, amino, thio, hydroxy, cyano, and/or halo groups.

As used herein, “aryl” groups are cyclic aromatic hydrocarbons that do not contain heteroatoms. Aryl groups include monocyclic, bicyclic and polycyclic ring systems. Thus, aryl groups include, but are not limited to, phenyl, azulenyl, heptalenyl, biphenylenyl, indacenyl, fluorenyl, phenanthrenyl, triphenylenyl, pyrenyl, naphthacenyl, chrysenyl, biphenyl, anthracenyl, indenyl, indanyl, pentalenyl, and naphthyl groups. In some embodiments, aryl groups contain 6-14 carbons, and in others from 6 to 12 or even 6-10 carbon atoms in the ring portions of the groups. The phrase “aryl groups” includes groups containing fused rings, such as fused aromatic-aliphatic ring systems (e.g., indanyl, tetrahydronaphthyl, and the like). Aryl groups may be substituted or unsubstituted.

The term “microorganisms” as used herein refers to microbes capable of degrading hydrocarbons.

The term “paraffins” as used herein means branched or unbranched hydrocarbon alkanes. An unbranched paraffin is an n-paraffin; a branched paraffin is an isoparaffin.

The term “paraffinic” as used herein means both paraffins as defined above as well as predominantly hydrocarbon chains possessing regions that are alkane, either branched or unbranched, with mono- or di-unsaturation (i.e. one or two double bonds), halogenation from about 30 wt % to about 70 wt %, or where the hydrocarbon is both unsaturated and halogenated. However, the term does not describe a halogen on a carbon involved in a double bond.

The phrase “C₂+ chain branching” as used herein means alkyl branches wherein the alkyl group has two or more carbons; e.g. ethyl or isopropyl branches.

“Protecting” as used herein includes, but is not limited to, solvating, coating, cleaning, lubricating, or preserving a substance, surface, or composition.

“Orifice” as used herein encompasses holes, channels, fractures, and fissure; in other words, the term encompasses spaces of any three-dimensional length, width, and diameter that are not filled with solid material.

The present technology provides bio-based synthetic fluids as well as methods for making the fluids and methods that utilize the advantageous properties of the bio-based synthetic fluids, as discussed herein.

In an aspect, a method is provided involving altering the viscosity of bio-derived paraffins to produce a paraffinic fluid, where the altering step includes oligomerizing bio-derived paraffins, unsaturating bio-derived paraffins, chlorinating bio-derived paraffins, or a combination of any two or more thereof; the bio-derived paraffins are produced by hydrodeoxygenating a bio-based feed; the bio-based feed comprises bio-derived fatty acids, fatty acid esters, or a combination thereof; the bio-derived paraffins comprise n-paraffins; and the n-paraffins have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. The biodegradability may be about 42%, about 44%, about 46%, about 48%, about 50%, about 52%, about 54%, about 56%, about 58%, about 60%, about 62%, about 64%, about 66%, about 68%, about 70%, about 72%, about 74%, about 76%, about 78%, about 80%, and ranges between any two of these values or greater than any one of these values. In some embodiments, the paraffinic fluid contains below about 1 wt % total aromatics. The paraffinic fluid may contain aromatics in the amount of about 0.9 wt %, about 0.8 wt %, about 0.7 wt %, about 0.6 wt %, about 0.5 wt %, about 0.4 wt %, about 0.3 wt %, about 0.2 wt %, about 0.1 wt %, and ranges between any two of these values or below any one of these values. In some embodiments, the paraffinic fluid contain less than 0.1 wt % total aromatics. In some embodiments, the paraffinic fluid is free of benzene.

In some embodiments, the paraffinic fluid has a kinematic viscosity less than about 10 cSt at 40° C. In such embodiments, the paraffinic fluid may have a kinematic viscosity at 40° C. of about 9 cSt, about 8 cSt, about 7 cSt, about 6 cSt, about 5 cSt, about 4 cSt, about 3 cSt, about 2 cSt, about 1 cSt, and ranges in between any two of these values or below any one of these values. In some embodiments, the paraffinic fluid has a kinematic viscosity greater than about 10 cSt at 40° C. In such embodiments, the paraffinic fluid may have a kinematic viscosity at 40° C. of about 12 cSt, about 14 cSt, about 16 cSt, about 18 cSt, about 20 cSt, about 22 cSt, about 24 cSt, about 26 cSt, about 28 cSt, about 30 cSt, and ranges in between any two of these values or greater than any one of these values. In some embodiments, the paraffinic fluid has a kinematic viscosity greater than about 20 cSt at 40° C.

Bio-Based Feed:

Bio-derived fatty acids, fatty acid esters, or combinations thereof, are utilized as the bio-based feed for making the fluids described throughout this application. The bio-derived fatty acids, fatty acid esters, or combinations thereof include algae oils, beef tallow, camelina oil, canola/rapeseed oil, castor oil, choice white grease, coconut oil, coffee bean oil, corn oil, fish oils, hemp oil, Jatropha oil, linseed oil, mustard oil, palm oil, poultry fat, soybean oil, sunflower oil, tall oil, tall oil fatty acid, Tung oil, used cooking oils, yellow grease, products of the food industry, or combinations of any two or more thereof. In some embodiments, the bio-derived fatty acids, fatty acid esters, or combinations thereof include soybean oil, corn oil, cottonseed oil, canola oil, coconut oil, sunflower oil, palm oil, palm kernel oil, rapeseed oil, or a combination of any two or more thereof.

In their natural form, most of these fats and oils contain phosphorus as well as metals such as calcium, magnesium, sodium, potassium, iron, and copper. Additionally, most also contain nitrogen compounds such as chlorophyll or amino acids. When the level of phosphorus is greater than about 40 wppm, and total metals greater than about 30 wppm, the fats and oils may be subjected to treatment steps including, but not limited to, acid degumming, neutralization, bleaching, or a combination of any two or more thereof. Acid degumming involves contacting the fat/oil with concentrated aqueous acids. Exemplary acids are phosphoric, citric, and maleic acids. This pretreatment step removes metals such as calcium and magnesium in addition to phosphorus. Neutralization is typically performed by adding a caustic (referring to any base, such as aqueous NaOH) to the acid-degummed fat/oil. The process equipment used for acid degumming and neutralization includes high shear mixers and disk stack centrifuges.

Bleaching typically involves contacting the degummed fat/oil with adsorbent clay and filtering the spent clay through a pressure leaf filter. Use of synthetic silica instead of clay is reported to provide improved adsorption. The bleaching step removes chlorophyll and much of the residual metals and phosphorus. Any soaps that may have been formed during the caustic neutralization step (i.e. by reaction with free fatty acids) are also removed during the bleaching step. The aforementioned treatment processes are known in the art and described in the patent literature, including but not limited to U.S. Pat. Nos. 4,049,686, 4,698,185, 4,734,226, and 5,239,096. It should be recognized by those skilled in the art that other fat/oil treatment methods, including those involving alternate physical, thermal, and chemical processes, may be adapted to pretreatment of a bio-based feed.

Hydrodeoxygenation:

The bio-based feed is subjected to hydrodeoxygenation (HDO) in a catalytic reactor wherein the fatty acids and/or fatty acid esters are converted to straight-chain paraffins. In hydrodeoxygenation, the oxygen atoms of the fatty acid/ester are removed through hydrogenolysis to form water, while the unsaturated carbon-carbon double bonds of the fatty acid chains are simultaneously hydrogenated. HDO may be accompanied by decarbonylation and decarboxylation reactions (wherein the oxygen atom is removed as CO and CO₂ respectively). The HDO reaction takes place at temperatures from about 200° C. to about 400° C., and hydrogen partial pressure between about 20 bar to about 160 bar. The HDO reaction may occur at a temperature of about 220° C., 240° C., 260° C., 280° C., 300° C., 320° C., 340° C., 360° C., 380° C., and ranges between any two of these values or above any one of these values. In some embodiments, temperature range is from about 260° C. to about 370° C. The HDO reaction may occur at a hydrogen partial pressure of about 30 bar, 40 bar, 50 bar, 60 bar, 70 bar, 80 bar, 90 bar, 100 bar, 110 bar, 120 bar, 130 bar, 140 bar, 150 bar, and ranges between any two of these values or above any one of these values. In some embodiments, the pressure range is from about 30 bar to about 130 bar. Suitable catalysts for the HDO process include sulfided forms of hydrogenation metals from Group VIB and Group VIII of the periodic table. Examples of suitable mono-metallic, bi-metallic, and tri-metallic catalysts include Mo, Ni, Co, W, CoMo, NiMo, NiW, NiCoMo. These catalysts may be supported on alumina, or alumina modified with oxides of silicon and/or phosphorus. These catalysts may be purchased in the reduced sulfide form, or more commonly purchased as metal oxides and sulfided during startup. To ensure these catalysts remain in the reduced sulfide form required for desired activity/selectivity balance, use of a “sulfur spike” compound such as dimethyl disulfide may be utilized. Fixed-bed and/or slurry reactor systems and operating conditions may be used. In some embodiments, continuous reactor systems are used. In some embodiments, continuous fixed-bed reactors are used. In continuous fixed-bed reactor systems, the liquid hourly space velocity (LHSV) is between about 0.2 h⁻¹ and about 10 h⁻¹, and the hydrogen gas-to-oil ratio (GOR at standard conditions) is between about 200 NL/L and about 1600 NL/L. The LHSV may be about 0.3 h⁻¹, about 0.4 h⁻¹, about 0.5 h⁻¹, about 0.6 h⁻¹, about 0.7 h⁻¹, about 0.8 h⁻¹, about 0.9 h⁻¹, about 1.0 h⁻¹, about 1.2 h⁻¹, about 1.4 h⁻¹, about 1.6 h⁻¹, about 1.8 h⁻¹, about 2.0 h⁻¹, about 2.2 h⁻¹, about 2.4 h⁻¹, about 2.6 h⁻¹, about 2.8 h⁻¹, about 3.0 h⁻¹, about 3.0 h⁻¹, about 3.2 h⁻¹, about 3.4 h⁻¹, about 3.6 h⁻¹, about 3.8 h⁻¹, about 4.0 h⁻¹, about 4.2 h⁻¹, about 4.4 h⁻¹, about 4.6 h⁻¹, about 4.8 h⁻¹, about 5.0 h⁻¹, about 5.2 h⁻¹, about 5.4 h⁻¹, about 5.6 h⁻¹, about 5.8 h⁻¹, about 6.0 h⁻¹, about 6.2 h⁻¹, about 6.4 h⁻¹, about 6.6 h⁻¹, about 6.8 h⁻¹, about 7.0 h⁻¹, about 7.2 h⁻¹, about 7.4 h⁻¹, about 7.6 h⁻¹, about 7.8 h⁻¹, about 8.0 h⁻¹, about 8.2 h⁻¹, about 8.4 h⁻¹, about 8.6 h ⁻¹, about 8.8 h ⁻¹, about 9.0 h⁻¹, about 9.2 h⁻¹, about 9.4 h⁻¹, about 9.6 h⁻¹, about 9.8 h⁻¹, and ranges between any two of these values or above any one of these values. In some embodiments with continuous fixed-bed reactor systems, the LHSV is from about 0.5 h⁻¹ to about 5.0 h⁻¹. The GOR may be about 250 NL/L, 300 NL/L, 350 NL/L, 400 NL/L, 450 NL/L, 500 NL/L, 550 NL/L, 600 NL/L, 650 NL/L, 700 NL/L, 750 NL/L, 800 NL/L, 850 NL/L, 900 NL/L, 950 NL/L, 1000 NL/L, 1050 NL/L, 1100 NL/L, 1150 NL/L, 1200 NL/L, 1250 NL/L, 1300 NL/L, 1350 NL/L, 1400 NL/L, 1450 NL/L, 1500 NL/L, 1550 NL/L, and ranges between any two of these values or above any one of these values. In some embodiments with continuous fixed-bed reactor systems, GOR is from about 400 NL/L to about 1400 NL/L.

The reactor effluent is directed to a high pressure separator for separating the gas stream containing unreacted hydrogen and gas phase byproducts such as water, CO, CO₂, H₂S, NH₃, and propane from the liquid HDO products. The gas is then cooled and directed to a three-phase cold separator drum. There a water stream with dissolved carbonate, bisulfide, and ammonium salts, a hydrocarbon stream containing light hydrocarbons, and a hydrogen rich gas stream are separated. The hydrogen rich gas is optionally scrubbed to remove the gas phase byproducts and recycled to the reactor. The liquid HDO product from the high pressure separator may also be partially recycled to the reactor to dilute the reactive bio-based feed to the exothermic HDO reactor.

Those skilled in the art recognize that variations to these operating conditions may be made based on purity of available hydrogen gas and to ensure proper three-phase (H₂ gas/liquid feed/solid catalyst) contacting regime within the reactor. The liquid paraffin product composition obtained from subjecting most fatty acid/ester bio-based feeds to HDO is a hydrocarbon composition rich in n-paraffins in the C₁₁ to C₂₂ range. The HDO product contains between about 80 wt % and 100 wt % n-paraffins, between about 0 wt % and about 20 wt % isoparaffins, between about 0 wt % and about 10 wt % cycloparaffins (also called naphthenes or naphthenics), between about 0 wt % and about 10% wt % olefins, and below about 1 wt % total aromatics. It is important to note that the method does not involve more severe aromatic hydrogenation conditions. The HDO product may contain n-paraffins in the amount of about 82 wt %, about 84 wt %, about 86 wt %, about 88 wt %, about 90 wt %, about 92 wt %, about 94 wt %, about 96 wt %, about 98 wt %, and ranges between any two of these values or above any one of these values. The n-paraffins have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. The biodegradability may be about 42%, about 44%, about 46%, about 48%, about 50%, about 52%, about 54%, about 56%, about 58%, about 60%, about 62%, about 64%, about 66%, about 68%, about 70%, about 72%, about 74%, about 76%, about 78%, about 80%, and ranges between any two of these values or greater than any one of these values. The n-paraffins have a kinematic viscosity of less than about 10 cSt at 40° C. The n-paraffins may have a kinematic viscosity at 40° C. of about 9 cSt, about 8 cSt, about 7 cSt, about 6 cSt, about 5 cSt, about 4 cSt, about 3 cSt, about 2 cSt, about 1 cSt, and ranges in between any two of these values or below any one of these values.

The HDO product may contain cycloparaffins in the amount of about 1 wt %, about 2 wt %, about 3 wt %, about 4 wt %, about 5 wt %, about 6 wt %, about 7 wt %, about 8 wt %, about 9 wt %, and ranges between any two of these values or below any one of these values. The HDO product may contain aromatics in the amount of about 0.9 wt %, about 0.8 wt %, about 0.7 wt %, about 0.6 wt %, about 0.5 wt %, about 0.4 wt %, about 0.3 wt %, about 0.2 wt %, about 0.1 wt %, and ranges between any two of these values or below any one of these values. In some embodiments, the HDO product contains less than 0.1 wt % total aromatics. In some embodiments, the HDO product is free of benzene. The HDO product has a kinematic viscosity of less than about 10 cSt at 40° C. The HDO product may have a kinematic viscosity at 40° C. of about 9 cSt, about 8 cSt, about 7 cSt, about 6 cSt, about 5 cSt, about 4 cSt, about 3 cSt, about 2 cSt, about 1 cSt, and ranges in between any two of these values or below any one of these values.

The HDO product may be distilled to yield a synthetic renewable drilling base fluid in the C₁₆-C₁₈ range. This fluid has a flash point greater than about 100° C., a kinematic viscosity in the range of about 3 cSt to about 4 cSt at 40° C., a pour point of about 16° C. to about 20° C., high thermal and oxidative stability due to paraffinic structure (i.e. having a total insoluble content of 0.2 mg/100 mL or less according to the ASTM D2274 accelerated oxidative aging method when 20 wppm or more anti-oxidant is added to the fluid), low aquatic toxicity and ecotoxicity (i.e. having an LC₅₀ value of 3.5 mg/L or higher where LC₅₀ is the concentration at which half a population of the organism dies of ingesting the fluid, and is typically the average of 24 hour, 48 hour, and 72 hour exposure tests on Daphia magna, Pimephales promelas, or Rainbow Trout), and a biodegradability greater than about 40% according to ASTM D5864-05, incorporated herein by reference. ASTM D5864-05 measures how much of a material breaks down into CO₂ by microorganisms over a period of 23 days. In contrast to the paraffins of this application, typical petroleum-based mineral oils have biodegradability in the 15-35% range, while synthetic oils like poly alpha-olefins (PAOs) have biodegradability in the 5-30% range. Organic compounds with low biodegradability (i.e. less than about 40% biodegradability) are said to bioaccumulate. Bioaccumulation tends to magnify the toxic effect of chemicals on the environment.

Hydroisomerization of Bio-Based Paraffins:

The HDO paraffins may be subjected to hydroisomerization to provide a hydroisomerized product. The hydroisomerized product includes methyl-branched paraffins in the C₁₆-C₁₈ range with low pour point, high thermal/oxidative stability, and low ecotoxicity. Hydroisomerization is conducted over a bifunctional catalyst at temperatures in the range of about 200° C. to about 500° C. The hydroisomerization may be conducted at a temperature of about 220° C., about 240° C., about 260° C., about 280° C., about 300° C., about 320° C., about 340° C., about 360° C., about 380° C., about 400° C., about 420° C., about 440° C., about 460° C., about 480° C., and ranges between any two of these values or above any one of these values. Bifunctional catalysts are those having a hydrogenation-dehydrogenation activity from a Group VIB and/or Group VIII metal, and acidic activity from an amorphous or crystalline support such as amorphous silica-alumina (ASA), silicon-aluminum-phosphate (SAPO) molecular sieve, or aluminum silicate zeolite (ZSM). In some embodiments, the hydroisomerization catalysts include Pt/Pd-on-ASA, and Pt-on-SAPO-11.

In some embodiments, hydroisomerization is conducted in continuous fixed-bed reactors. In such embodiments, the hydrogen partial pressure for hydroisomerization is in the range between about 30 bar and about 160 bar, GORs are in the range of about 100 NL/L to about 1,000 NL/L, and LHSV in the range from about 0.2 hr⁻¹ to about 5 hr⁻¹. In some embodiments, the hydrogen partial pressure for hydroisomerization is about 40 bar, about 50 bar, about 60 bar, about 70 bar, about 80 bar, about 90 bar, about 100 bar, about 110 bar, about 120 bar, about 130 bar, about 140 bar, about 150 bar, and ranges between any two of these values or above any one of these values. In some embodiments, the GOR may be about 150 NL/L, about 200 NL/L, about 250 NL/L, 300 NL/L, 350 NL/L, 400 NL/L, 450 NL/L, 500 NL/L, 550 NL/L, 600 NL/L, 650 NL/L, 700 NL/L, 750 NL/L, 800 NL/L, 850 NL/L, 900 NL/L, 950 NL/L, and ranges between any two of these values or above any one of these values. The LHSV may be about 0.3 h⁻¹, about 0.4 h⁻¹, about 0.5 h⁻¹, about 0.6 h⁻¹, about 0.7 h⁻¹, about 0.8 h⁻¹, about 0.9 h⁻¹, about 1.0 h⁻¹, about 1.2 h⁻¹, about 1.4 h⁻¹, about 1.6 h⁻¹, about 1.8 h⁻¹, about 2.0 h⁻¹, about 2.2 h⁻¹, about 2.4 h⁻¹, about 2.6 h⁻¹, about 2.8 h⁻¹, about 3.0 h⁻¹, about 3.0 h⁻¹, about 3.2 h⁻¹, about 3.4 h⁻¹, about 3.6 h⁻¹, about 3.8 h⁻¹, about 4.0 h⁻¹, about 4.2 h⁻¹, about 4.4 h⁻¹, about 4.6 h⁻¹, about 4.8 h⁻¹, and ranges between any two of these values or above any one of these values.

In an embodiment, the HDO product is hydroisomerized according to the conditions described herein using Pt/SAPO-11 catalyst. The hydroisomerizate is preferably stripped of light hydrocarbons in order to raise the flash point above 60° C. The flash point may be above 70° C., above 80° C., above 90° C., or above 100° C. The hydroisomerized product has a ratio of isoparaffins-to-normal paraffins in the range of about 1:1 to about 30:1. The ratio of isoparaffins-to-normal paraffins may be about 2:1, about 3:1, about 4:1, about 5:1, about 6:1, about 7:1, about 8:1, about 9:1, about 10:1, about 11:1, about 12:1, about 13:1, about 14:1, about 15:1, about 16:1, about 17:1, about 18:1, about 19:1, about 20:1, about 21:1, about 22:1, about 23:1, about 24:1, about 25:1, about 26:1, about 27:1, about 28:1, about 29:1, and ranges between any two of these values or above any one of these values. In some embodiments, the ratio of isoparaffins-to-normal paraffins is between about 5:1 and about 20:1. In the hydroisomerized product at least 80 wt % of the isoparaffins are mono-methyl branched paraffins. The mono-methyl branched paraffins may be about 81 wt %, about 82 wt %, about 83 wt %, about 84 wt %, about 85 wt %, about 86 wt %, about 87 wt %, about 88 wt %, about 89 wt %, about 90 wt %, about 91 wt %, about 92 wt %, about 93 wt %, about 94 wt %, about 95 wt %, about 96 wt %, about 97 wt %, about 98 wt %, about 99 wt %, and ranges between any two of these values or above any one of these values. Examples of the mono-methyl branched paraffins in the hydroisomerized HDO product include 4-methyl heptadecane, 3-methyl hexadecane, and 2-methyl pentadecane. Of the mono-methyl branched isoparaffins, less than 30 wt % are terminal branched (i.e. 2-methyl branched). In some embodiments, less than 20 wt % of the mono-methyl branched isoparaffins are terminal branched. In some embodiments, less than 15 wt % of the mono-methyl branched isoparaffins are terminal branched. In some embodiments, less than 10 wt % of the mono-methyl branched isoparaffins are terminal branched. In some embodiments, less than 5 wt % of the mono-methyl branched isoparaffins are terminal branched. It is important to note that the method does not involve more severe aromatic hydrogenation conditions.

The isoparaffins have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. The biodegradability may be about 42%, about 44%, about 46%, about 48%, about 50%, about 52%, about 54%, about 56%, about 58%, about 60%, about 62%, about 64%, about 66%, about 68%, about 70%, about 72%, about 74%, about 76%, about 78%, about 80%, and ranges between any two of these values or greater than any one of these values. The isoparaffins have a kinematic viscosity of less than about 10 cSt at 40° C. The isoparaffins may have a kinematic viscosity at 40° C. of about 9 cSt, about 8 cSt, about 7 cSt, about 6 cSt, about 5 cSt, about 4 cSt, about 3 cSt, about 2 cSt, about 1 cSt, and ranges in between any two of these values or below any one of these values.

The hydroisomerized product may contain aromatics in the amount of about 0.9 wt %, about 0.8 wt %, about 0.7 wt %, about 0.6 wt %, about 0.5 wt %, about 0.4 wt %, about 0.3 wt %, about 0.2 wt %, about 0.1 wt %, and ranges between any two of these values or below any one of these values. In some embodiments, the hydroisomerized product contains less than 0.1 wt % total aromatics. In some embodiments, the hydroisomerized product is free of benzene. The hydroisomerized product has a kinematic viscosity of less than about 10 cSt at 40° C. The hydroisomerized product has a kinematic viscosity of less than about 10 cSt at 40 ° C. The hydroisomerized product may have a kinematic viscosity at 40° C. of about 9 cSt, about 8 cSt, about 7 cSt, about 6 cSt, about 5 cSt, about 4 cSt, about 3 cSt, about 2 cSt, about 1 cSt, and ranges in between any two of these values or below any one of these values.

Due the presence of mostly internal mono-methyl branched paraffins, the hydroisomerized HDO product of this technology has an excellent balance of properties for use as drilling and/or hydraulic fracturing fluids. The pour point of the hydroisomerized fluid of this embodiment is at most −10° C. The pour point may be at most about −15° C., at least about −20° C., at most about −25° C., at most about −30° C., at most about −35° C., at most about −40° C., or at most about −45° C. The thermo-oxidative stability of the fluid may be measured by amount of insolubles formed upon heating and reported as mg/100 mL according to ASTM D2274. For example, the stability thus measured can be as high as 20 mg/100 mL for fluids with inferior oxidative stability properties, such as fatty acid esters. The lower the concentration of insolubles formed, the higher the thermo-oxidative stability of the fluid. The ASTM D2274 oxidative stability of the fluid produced by hydroisomerization of the HDO product as described herein is between about 0 mg/100 mL and about 2 mg/100 mL upon addition of up to 20 wppm anti-oxidant. Preferred anti-oxidants for the bio-based hydrocarbon fluids of this technology are hindered phenols, such as butyrated hydroxy toluene (BHT). Other examples of suitable anti-oxidants for the bio-based synthetic hydrocarbon fluids of this invention include 2,4-dimethyl-6-t-butylphenol, 2,6-di-t-butyl-4-methylphenol, 2- and 3-t-butyl-4-hydroxyanisol (BHA), 2,6-distyrenated p-cresol, 2,6-di-t-butylphenol, 2,6-di-t-butyl-4-sec-butylphenol, 2,6-di-t-butyl-4-nonylphenol, 2,4-bis-(n-octylthio)-6-(4-hydroxy-3′,5′-di-t-butylanilino)-1,3,5-triazine, 2,4-bis-(octylthiomethyl)-6-methylphenol, 2,6-di-t-butyl-4-ethylphenol, 2,4-dimethyl-6-t-butylphenol, the butylated reaction product of p-cresol and dicylcopentadiene, the mixed methylenic bridged adducts of alkylated phenol and dodecane thiol, tetrakis methylene (3,5-di-t-butyl-4-hydroxyhydrocinnamate) methane, 1,3,5-trimethyl-2,4,6-tris (3,5-di-t-butyl-4-hydroxybenzyl) benzene, tris (3,5-di-t-butyl-4-hydroxybenzyl) isocyanurate, and mixtures of any two or more thereof of the recited anti-oxidants.

Chlorinating Bio-Based Paraffins:

Paraffin chlorination according to the present technology is one way of increasing the viscosity of a paraffinic fluid while reducing crystallinity and hence lowering the paraffin pour point. For example, the HDO product does not have the required viscosity and pour point for use, by itself, in such industrial processing fluid applications as metal-working.

The HDO product and/or the hydroisomerized product may be chlorinated in a batch reactor by sparging pure chlorine gas into the liquid at a temperature in the range between about 60° C. and about 150° C. The temperature of the chlorination reaction may be about 65° C., about 70° C., about 80° C., about 85° C., about 90° C., about 95° C., about 100° C., about 105° C., about 110° C., about 115° C., about 120° C., about 125° C., about 130° C., about 140° C., about 145° C., and ranges in between any two of these values or greater than any one of these values. In some embodiments, the temperature is in the range between about 80° C. and about 120° C. Chlorination is an exothermic reaction and cooling is necessary. Generally catalysts are not necessary at these temperatures, but in some embodiments UV light is used to accelerate the reaction. Once the desired degree of chlorination, typically between about 30 wt % and about 70 wt %, and viscosity has been achieved, the chlorine supply is discontinued and the reactor purged with air or nitrogen to remove excess chlorine and hydrochloric acid gas. Hydrochloric acid is a co-product of the paraffin chlorination process.

The chlorinated paraffins, i.e. the chlorinated product, can be used as an industrial process fluid for metal-working lubricants, as plasticizers, flame-retardants, and fat liquors for leather. Plasticizers are generally used to make rigid polymers like PVC soft and rubbery. Addition of chlorinated paraffins also imparts flame-retardancy to the polymer compound. Fat liquors are fluids that are used to improve the life and appearance of articles made of leather, such as jackets, handbags, and shoes. In some embodiments, the chlorinated product is used as a protecting agent, a cleaning agent, or a combination of both. In some embodiments, the chlorinated product acts as a flame retardant. In some embodiments, the chlorinated product is used to clean fabric, metal, or plastic.

The chlorinated product has a kinematic viscosity of greater than about 10 cSt at 40° C. The chlorinated product may have a kinematic viscosity at 40° C. of about 12 cSt, about 14 cSt, about 16 cSt, about 18 cSt, about 20 cSt, about 22 cSt, about 24 cSt, about 26 cSt, about 28 cSt, about 30 cSt, and ranges in between any two of these values or greater than any one of these values. The chlorinated product is between about 30 wt % and about 70 wt % chlorine in the form of chlorine covalently bound to carbon. The amount of covalently bonded chlorine in the chlorinated product may be about 35 wt %, about 40 wt %, about 45 wt %, about 50 wt %, about 55 wt %, about 60 wt %, about 65 wt %, and ranges between any two of these values or greater than any one of these values. The chlorinated product has less than about 1 wt % aromatics. The chlorinated product may contain aromatics in the amount of about 0.9 wt %, about 0.8 wt %, about 0.7 wt %, about 0.6 wt %, about 0.5 wt %, about 0.4 wt %, about 0.3 wt %, about 0.2 wt %, about 0.1 wt %, and ranges between any two of these values or below any one of these values. In some embodiments, the chlorinated product contains less than 0.1 wt % total aromatics. In some embodiments, the chlorinated product is free of benzene. In some embodiments, the chlorinated product is used as a protecting agent, a cleaning agent, or a combination of both. In some embodiments, the chlorinated product acts as a flame retardant. In some embodiments, the chlorinated product is used to clean fabric, metal, or plastic.

Dehydrochlorinadon of Bio-Derived Paraffins:

The chlorinated products may optionally be subjected to dehydrochlorination, wherein the chlorine is removed as hydrochloric acid. As an example, in embodiments where the chlorinated product is exclusively made from the HDO product, dehydrochlorination yields a linear olefin composition having a carbon number range similar to the HDO paraffin. The dehydrochlorination reaction takes place over silica or bauxite at temperatures in the 360° C.-700° C. range. The reaction may take place at a temperature of about 380° C., about 400° C., about 420° C., about 440° C., about 460° C., about 480° C., about 500° C., about 550° C., about 600° C., about 650° C., and ranges in between any two of these values or above any one of these values. In some embodiments, the reaction takes place at temperature in the range from about 400° C. to about 600° C. Dehydrochlorination may proceed in the range from about 68% conversion to about 100% conversion. Dehydrochlorination can proceed to about 70% conversion, about 75% conversion, about 80% conversion, about 85% conversion, about 90% conversion, about 95% conversion, about 98% conversion, about 99% conversion, and ranges in between any two of these values or above any one of these values. As such, the dehydrochlorination reactor product from dehydrochlorination of the HDO product is a C₁₆/C₁₈ linear hydrocarbon composition comprising up to 100% internal olefins, characterized by higher biodegradability than saturated hydrocarbons. This olefinic composition has a lower pour point and higher lubricity than the equivalent paraffin composition, making it particularly well-suited for drilling and hydraulic fracturing fluid formulations.

The olefinic composition has a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. The biodegradability may be about 42%, about 44%, about 46%, about 48%, about 50%, about 52%, about 54%, about 56%, about 58%, about 60%, about 62%, about 64%, about 66%, about 68%, about 70%, about 72%, about 74%, about 76%, about 78%, about 80%, and ranges between any two of these values or greater than any one of these values. The olefinic composition has a kinematic viscosity of less than about 10 cSt at 40° C. The olefinic composition may have a kinematic viscosity at 40° C. of about 9 cSt, about 8 cSt, about 7 cSt, about 6 cSt, about 5 cSt, about 4 cSt, about 3 cSt, about 2 cSt, about 1 cSt, and ranges in between any two of these values or below any one of these values. The olefinic composition may contain aromatics in the amount of about 0.9 wt %, about 0.8 wt %, about 0.7 wt %, about 0.6 wt %, about 0.5 wt %, about 0.4 wt %, about 0.3 wt %, about 0.2 wt %, about 0.1 wt %, and ranges between any two of these values or below any one of these values. In some embodiments, the olefinic composition contains less than 0.1 wt % total aromatics. In some embodiments, the olefinic composition is free of benzene. In some embodiments, the olefinic composition is used as a hydraulic fracturing fluid, as a drilling fluid, or a combination of the two.

Dehydrogenation of Bio-Derived Paraffins:

The paraffinic fluid, for example the HDO product and/or the hydroisomerization product, may be subjected to dehydrogenation to produce a olefinic fluid with an improved balance of biodegradability, lubricity, thermo-oxidative stability, ecotoxicity, and pour point, for drilling base fluids. The reaction takes place at a temperature in the range from about 360° C. to about 660° C. The reaction may take place at about 380° C., about 400° C., about 420° C., about 440° C., about 460° C., about 480° C., about 500° C., about 520° C., about 540° C., about 560° C., about 580° C., about 600° C., about 620° C., about 640° C., and ranges between any two of these values or above any one of these values. In some embodiments, the reaction takes place in a temperature in the range from about 440° C. to about 580° C. The reaction is endothermic and is favored at low pressures. Typical operating pressures are in the range from about 1 bar to about 20 bar. The operating pressure may be about 2 bar, about 3 bar, about 4 bar, about 5 bar, about 6 bar, about 7 bar, about 8 bar, about 9 bar, about 10 bar, about 11 bar, about 12 bar, about 13 bar, about 14 bar, about 15 bar, about 16 bar, about 17 bar, about 18 bar, about 19 bar, and ranges between any two of these values or above any one of these values. In some embodiments, the operating pressure is from about 2 bar to about 12 bar. At these conditions, the hydrocarbons are in vapor phase. Generally base metals and noble metal catalysts from Groups VIB and VIII that have hydrogenation-dehydrogenation activity provide a low activation energy mechanism for paraffin dehydrogenation. Such metals include Pt, Pd, Rh, Ru, Ir, Os, and Re. The reaction is carried out in gas phase at high temperatures and low pressures. Preferred catalyst systems for paraffin dehydrogenation include alkali and alkaline earth metal promoters as well. A preferred catalyst for the system is platinum/lithium on alumina.

In an embodiment, the HDO paraffins are pressurized to about 10 bar and preheated to about 580° C. before entering a dehydrogenation reactor. It is important to note that the conditions provided in this embodiment are applicable to the dehydrogenation of the hydroisomerized product described earlier. The reactor is packed with Pt/Li-on-alumina catalyst. The reactor geometry is selected to provide low pressure drop while ensuring sufficient contact time to achieve desired conversion, and preferably approach the thermodynamic equilibrium conversion for the endothermic reactions. Preferred contact times are expressed by liquid hourly space velocities (LHSV) in the range of about 1 h⁻¹ to about 10 h⁻¹. The LHSV may be about 1.2 h⁻¹, about 1.4 h⁻¹, about 1.6 h⁻¹, about 1.8 h⁻¹, about 2.0 h⁻¹, about 2.2 h⁻¹, about 2.4 h⁻¹, about 2.6 h⁻¹, about 2.8 h⁻¹, about 3.0 h⁻¹, about 3.0 h⁻¹, about 3.2 h⁻¹, about 3.4 h⁻¹, about 3.6 h⁻¹, about 3.8 h⁻¹, about 4.0 h⁻¹, about 4.2 h⁻¹, about 4.4 h⁻¹, about 4.6 h⁻¹, about 4.8 h⁻¹, about 5.0 h⁻¹, about 5.2 h⁻¹, about 5.4 h⁻¹, about 5.6 h⁻¹, about 5.8 h⁻¹, about 6.0 h⁻¹, about 6.2 h⁻¹, about 6.4 h⁻¹, about 6.6 h⁻¹, about 6.8 h⁻¹, about 7.0 h⁻¹, about 7.2 h⁻¹, about 7.4 h⁻¹, about 7.6 h⁻¹, about 7.8 h⁻¹, about 8.0 h⁻¹, about 8.2 h⁻¹, about 8.4 h⁻¹, about 8.6 h⁻¹, about 8.8 h⁻¹, about 9.0 h⁻¹, about 9.2 h⁻¹, about 9.4 h ¹, about 9.6 h ¹, about 9.8 h⁻¹, and ranges between any two of these values or above any one of these values. It should be noted that although space velocities are expressed in terms of liquid feed, in some embodiments of the dehydrogenation conditions the reactor feed and products are in the vapor phase. In some embodiments, a plurality of reactors is configured in series, with provisions for heating each reactor feed. In some embodiments, between about 5 wt % and about 40 wt % of the HDO n-paraffins are converted to linear olefins. The conversion of HDO n-paraffins to linear olefins may be about 10 wt %, about 15 wt %, about 20 wt %, about 25 wt %, about 30 wt %, about 35 wt %, and ranges in between any two of these values or above any one of these values. In some embodiments, between about 10 wt % and about 30 wt % of the HDO n-paraffins are converted to linear olefins. The reactor effluent is cooled to condense a linear hydrocarbon product composition from hydrogen, where the linear hydrocarbon product composition is primarily in the C₁₆-C₁₈ range. The hydrogen may be partially recycled to the reactor to mitigate coking in the reactor. A hydrogen-to-hydrocarbon mole ratio of about 1:1 to about 20:1 is utilized. The hydrogen-to-hydrocarbon mole ratio may be about 2:1, about 3:1, about 4:1, about 5:1, about 6:1, about 7:1, about 8:1, about 9:1, about 10:1, about 11:1, about 12:1, about 13:1, about 14:1, about 15:1, about 16:1, about 17:1, about 18:1, about 19:1, and ranges between any two of these values or above any one of these values. In some embodiments, the hydrogen-to-hydrocarbon mole ratio is from about 8:1 to about 12:1.

The liquid product of this embodiment of the dehydrogenation of the HDO product is a straight-chain hydrocarbon composition comprising of n-paraffins and linear olefins. The composition comprises 50-90 wt % n-paraffins in the C₁₆-C₁₈ range, 10-40 wt % C₁₆-C₁₈ linear internal olefins in the C₁₆-C₁₈ range, and 0-10 wt % linear alpha olefins in the C₁₆-C₁₈ range. The composition may have n-paraffins in the C₁₆-C₁₈ range in the amount of about 55 wt %, about 60 wt %, about 65 wt %, about 70 wt %, about 75 wt %, about 80 wt %, about 85 wt %, and ranges in between any two of these values or below any one of these values. The composition may have linear internal olefins in the C₁₆-C₁₈ range in the amount of about 15 wt %, about 20 wt %, about 25 wt %, about 30 wt %, about 35 wt %, and ranges between any two of these values or above any one of these values. The composition may have linear alpha olefins in the C₁₆-C₁₈ range in the amount of about 0 wt % to about 5 wt % or about 5 wt % to about 10 wt %.

Due the presence of linear internal olefins, the pour point of the straight-chain hydrocarbon composition is lowered. Compared to fully saturated hydrocarbons, this composition offers superior biodegradability, making it attractive as a drilling base fluid.

The olefinic fluid has a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. The biodegradability may be about 42%, about 44%, about 46%, about 48%, about 50%, about 52%, about 54%, about 56%, about 58%, about 60%, about 62%, about 64%, about 66%, about 68%, about 70%, about 72%, about 74%, about 76%, about 78%, about 80%, and ranges between any two of these values or greater than any one of these values. The olefinic fluid has a kinematic viscosity of less than about 10 cSt at 40° C. The olefinic fluid may have a kinematic viscosity at 40° C. of about 9 cSt, about 8 cSt, about 7 cSt, about 6 cSt, about 5 cSt, about 4 cSt, about 3 cSt, about 2 cSt, about 1 cSt, and ranges in between any two of these values or below any one of these values. The olefinic fluid of the present technology may contain aromatics in the amount of about 0.9 wt %, about 0.8 wt %, about 0.7 wt %, about 0.6 wt %, about 0.5 wt %, about 0.4 wt %, about 0.3 wt %, about 0.2 wt %, about 0.1 wt %, and ranges between any two of these values or below any one of these values. In some embodiments, the olefinic fluid contains less than 0.1 wt % total aromatics. In some embodiments, the olefinic fluid is free of benzene. In some embodiments, the olefinic fluid is used as a hydraulic fracturing fluid, as a drilling fluid, or a combination of the two.

Acid-Catalyzed Oligomerization:

It is to be understood that the term “oligomerization” as used herein refers to the formation of a compound from 2, 3, 4, 5, 6, 7, 8, 9 or 10 monomers, where the compound formed by oligomerization is an “oligomer” or an “oligomerized product.” For example, a dimer is a compound made from the oligomerization of 2 monomers, a trimer is a compound made from the oligomerization of 3 monomers, and a tetramer is a compound made from the oligomerization of 4 monomers. The olefins produced by dehydrogenation of the bio-derived paraffins or by dehydrochlorination of the chlorinated product, described above, can be oligomerized to produce fluids having a higher average molecular weight, higher boiling range, and higher viscosity. Since most of the carbon-carbon double bonds in the linear olefins are mainly in the internal positions (as indicated in the aforementioned section describing the internal olefins), the branched dimers are characterized by mainly C₂+ chain branching. Such fluids, having a kinematic viscosity greater than about 10 cSt at 40° C. are excellently suited for various mineral oil and lubricating oil applications. The oligomerized product may have a kinematic viscosity at 40 ° C. of about 12 cSt, about 14 cSt, about 16 cSt, about 18 cSt, about 20 cSt, about 22 cSt, about 24 cSt, about 26 cSt, about 28 cSt, about 30 cSt, and ranges in between any two of these values or greater than any one of these values. In some embodiments, the oligomerized product has a kinematic viscosity greater than about 20 cSt at 40° C.

Acids for olefin oligomerization include, but are not limited to, Lewis acids such as boron trifluoride and aluminum trichloride. Heterogeneous catalysts such as zeolites are another class of catalysts for olefin oligomerization. The reactions are conducted in a continuous stirred tank reactor using between about 1 wt % and about 15 wt % of the Lewis acid catalyst based on a oligomerization reactor hydrocarbon feed basis. The Lewis acid catalyst may be at about 2 wt %, about 3 wt %, about 4 wt %, about 5 wt %, about 6 wt %, about 7 wt %, about 8 wt %, about 9 wt %, about 10 wt %, about 11 wt %, about 12 wt %, about 13 wt %, about 14 wt %, and ranges between any two of these values. In some embodiments, the Lewis acid catalyst is from about 2 wt % to about 8 wt %. The reactor operates at a temperature in about the 0° C. to 200° C. range, under about 1 bar to about 10 bar pressure. The reactor may operate at a temperature of about 10° C., about 20° C., about 30° C., about 40° C., about 50° C., about 60° C., about 70° C., about 80° C., about 90° C., about 100° C., about 110° C., about 120° C., about 130° C., about 140° C., about 150° C., about 160° C., about 170° C., about 180° C., about 190° C., and ranges in between any two of these values. In some embodiments, the temperature is from about 20° C. to about 120° C. The reactor may operate at a pressure of about 2 bar, about 3 bar, about 4 bar, about 5 bar, about 6 bar, about 7 bar, about 8 bar, about 9 bar, and ranges in between any two of these values or above any one of these values. Reactor residence times are in the range of about 20 minutes to about 120 minutes. The reactor residence time may be about 30 minutes, about 40 minutes, about 50 minutes, about 60 minutes, about 70 minutes, about 80 minutes, about 90 minutes, about 100 minutes, about 110 minutes, and ranges in between any two of these values. In some embodiments, the reactor residence time is from about 30 minutes to about 90 minutes. The reactor effluent includes products of the oligomerization reaction. Unreacted hydrocarbons, if present, may be separated from the oligomerized product. The oligomerization product is predominately dimers and tetramers of the linear internal olefins. In some embodiments, the dimers and tetramers are greater than 60 wt % of the oligomerized product. The oligomerization product of this embodiment includes long-chain branched hydrocarbons. The unreacted linear hydrocarbons include the paraffin feed to the dehydrogenation reactor and the olefinic fluid not reacted under acid-catalyzed oligomerization conditions.

The oligomerized product may include a dimer, trimer, tetramer, or a mixture of any two or more thereof. The oligomerized product of the present technology may contain aromatics in the amount of about 0.9 wt %, about 0.8 wt %, about 0.7 wt %, about 0.6 wt %, about 0.5 wt %, about 0.4 wt %, about 0.3 wt %, about 0.2 wt %, about 0.1 wt %, and ranges between any two of these values or below any one of these values. In some embodiments, the oligomerized product contains less than 0.1 wt % total aromatics. In some embodiments, the oligomerized product is free of benzene. The oligomerized product has a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. The biodegradability may be about 42%, about 44%, about 46%, about 48%, about 50%, about 52%, about 54%, about 56%, about 58%, about 60%, about 62%, about 64%, about 66%, about 68%, about 70%, about 72%, about 74%, about 76%, about 78%, about 80%, and ranges between any two of these values or greater than any one of these values. In some embodiments, the oligomerized product is used as a drilling fluid, a hydraulic fracturing fluid, a metal working fluid, a protecting agent, or a combination of any two or more thereof.

Peroxide-Initiated Oligomerization:

Organic peroxide treatment may be used to initiate oligomerization of HDO and/or hydroisomerized HDO products. As stated above, it is to be understood that the term “oligomerization” as used herein refers to the formation of a compound from 2, 3, 4, 5, 6, 7, 8, 9 or 10 monomers, where the compound formed by oligomerization is an “oligomer.” For example, a dimer is a compound made from the oligomerization of 2 monomers, a trimer is a compound made from the oligomerization of 3 monomers, and a tetramer is a compound made from the oligomerization of 4 monomers. The product composition, comprising dimers and co-dimers of the linear and/or branched paraffins, has a kinematic viscosity greater than about 10 cSt at 40 C. The product is thus well suited for use in various mineral oil and lubricating oil applications.

Organic peroxides generate free radicals that extract hydrogen atoms from secondary and tertiary carbons of the paraffinic hydrocarbons, providing free radical sites therein for subsequent coupling reactions. The organic peroxides for the reaction are of the formula R-O-O-R′ where R and R′ are each independently H, alkyl, or aryl. In some embodiments, organic peroxides for the reaction include dialkyl peroxides including, but not limited to, di-tert butyl peroxide (DTBP), 2,5-dimethyl 2,5-di(t-butylperoxy)hexane, dicumyl peroxide, dibenzoyl peroxide, dipropyl peroxide, ethyl propyl peroxide, tert-butyl tert-amyl peroxide, or combinations of any two or more thereof.

Peroxide-initiated oligomerization may be carried out in batch or continuous reactors. Preferred batch reactor embodiments are agitated tanks with provisions for heat transfer/temperature control. These include jackets, internal coils, or pump-around heat exchange. Continuous flow reactors include those approaching plug-flow behavior such as tubular reactors (including, but not limited to, static mixers) and fixed-bed vessels packed with inert media like ceramic balls. As with the batch reactors, these plug -flow reactors may include provisions for heat transfer/temperature control. A low capital cost embodiment of the continuous reactor for peroxide-initiated oligomerization is the jacketed pipe or the pipe-in-pipe reactor.

The reactor feed comprising HDO and/or hydroisomerized HDO paraffins includes between about 2 wt % and about 40 wt % organic peroxide and the reactor is controlled at a temperature from about 50° C. to about 250° C. The organic peroxide may be in the amount of about 3 wt %, about 4 wt %, about 5 wt %, about 6 wt %, about 7 wt %, about 8 wt %, about 9 wt %, about 10 wt %, about 12 wt %, about 14 wt %, about 16 wt %, about 18 wt %, about 20 wt %, about 22 wt %, about 24 wt %, about 26 wt %, about 28 wt %, about 30 wt %, about 32 wt %, about 34 wt %, about 36 wt %, about 38 wt %, and ranges between any two of these values or above any one of these values. In some embodiments, the organic peroxide is in the amount of about 5 wt % to about 20 wt %. The reactor temperature may be about 60° C., about 70° C., about 80° C., about 90° C., about 100° C., about 110° C., about 120° C., about 130 ° C., about 140° C., about 150° C., about 160° C., about 170° C., about 180° C., about 190° C., about 200° C., about 210° C., about 220° C., about 230° C., about 240° C., and ranges in between any two of these values. In some embodiments, the temperature is between about 70° C. and about 200° C. The reactor is controlled at a suitable pressure, high enough to ensure reactor contents are in liquid phase. This pressure is typically from about 1 bar to about 10 bar. The reactor may operate at a pressure of about 2 bar, about 3 bar, about 4 bar, about 5 bar, about 6 bar, about 7 bar, about 8 bar, about 9 bar, and ranges in between any two of these values or above any one of these values. Batch cycle times, or residence times of continuous flow reactors, are in the range from about 10 minutes to about 120 minutes. The reactor residence time may be about 10 minutes, about 20 minutes, about 30 minutes, about 40 minutes, about 50 minutes, about 60 minutes, about 70 minutes, about 80 minutes, about 90 minutes, about 100 minutes, about 110 minutes, and ranges in between any two of these values. In some embodiments, the reactor residence time is from about 20 minutes to about 90 minutes.

In the batch mode, all the peroxide may be charged at once following addition of the paraffinic feedstock. The peroxide may also be introduced in increments over the batch cycle time. In other embodiments of peroxide-initiated oligomerization, the organic peroxide is fed to the batch reactor continuously during all or a portion of the batch reaction cycle time, preferably using a metering pump or control valve. This mode of operation is also referred to as “semi-batch” in the art.

The reactor effluent comprises oligomerization products, mainly dimers and trimers of the HDO and/or hydroisomerization paraffins. The unreacted paraffins, making up between about 0 wt % and about 60 wt % of the effluent composition, are optionally stripped (preferably via atmospheric or vacuum distillation) to yield a oligomerized fluid product having a kinematic viscosity greater than about 10 cSt at 40° C. The oligomerized product may have a kinematic viscosity at 40° C. of about 12 cSt, about 14 cSt, about 16 cSt, about 18 cSt, about 20 cSt, about 22 cSt, about 24 cSt, about 26 cSt, about 28 cSt, about 30 cSt, and ranges in between any two of these values or greater than any one of these values. In some embodiments, the oligomerized product has a kinematic viscosity greater than about 20 cSt at 40° C. This product is well-suited for use in various lubricating applications where a combination of high thermal stability, low ecotoxicity, and good low temperature properties is desired. The unreacted paraffins in the effluent composition may be about 1 wt %, about 2 wt %, 3 wt %, about 4 wt %, about 5 wt %, about 6 wt %, about 7 wt %, about 8 wt %, about 9 wt %, about 10 wt %, about 12 wt %, about 14 wt %, about 16 wt %, about 18 wt %, about 20 wt %, about 22 wt %, about 24 wt %, about 26 wt %, about 28 wt %, about 30 wt %, about 32 wt %, about 34 wt %, about 36 wt %, about 38 wt %, about 40 wt %, about 50 wt % and ranges between any two of these values or above any one of these values.

The oligomerized product may include a dimer, trimer, tetramer, or a mixture of any two or more thereof. The oligomerized product has a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. The biodegradability may be about 42%, about 44%, about 46%, about 48%, about 50%, about 52%, about 54%, about 56%, about 58%, about 60%, about 62%, about 64%, about 66%, about 68%, about 70%, about 72%, about 74%, about 76%, about 78%, about 80%, and ranges between any two of these values or greater than any one of these values. The oligomerized product of the present technology may contain aromatics in the amount of about 0.9 wt %, about 0.8 wt %, about 0.7 wt %, about 0.6 wt %, about 0.5 wt %, about 0.4 wt %, about 0.3 wt %, about 0.2 wt %, about 0.1 wt %, and ranges between any two of these values or below any one of these values. In some embodiments, the oligomerized product contains less than 0.1 wt % total aromatics. In some embodiments, the oligomerized product is free of benzene. In some embodiments, the oligomerized product is used as a drilling fluid, a hydraulic fracturing fluid, a metal working fluid, a protecting agent, or a combination of any two or more thereof.

In another aspect, a method is provided involving protecting a substance by applying the above-described paraffinic fluids. In the method, the paraffinic fluid includes a hydrodeoxygenated product; where the hydrodeoxygenated product is produced by hydrodeoxygenating a bio-derived feed; the bio-derived feed comprises bio-derived fatty acids, fatty acid esters, or a combination thereof; the hydrodeoxygenated product comprises n-paraffins; the paraffinic fluid contains less than 1 wt % aromatics; and the n-paraffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least 40% after about 23 days of exposure to microorganisms. In some embodiments, the hydrodeoxygenated product includes n-paraffins in the range of about 80 wt % to about 100 wt %; cycloparaffins in the range of about 0 wt % to about 10 wt %; less than about 1 wt % total aromatics. In some embodiments, the paraffinic fluid further includes a hydroisomerized product produced by at least partially hydroisomerizing the hydrodeoxygenated product; where the hydroisomerized product comprises isoparaffins where at least about 80 wt % of the isoparaffins are mono-methyl branched paraffins; the mono-methyl branched paraffins comprise less than about 30 wt % terminal branched isoparaffins; and the isoparaffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms.

Thus, in some embodiments of the method, the substance is a food crop, a metal, or wood. In some embodiments, protecting involves solvating the substance. In such embodiments, the substance includes pesticides, herbicides, paints, inks, or coatings. In some embodiments of the method, protecting involves cleaning the substance with the paraffinic fluid In such embodiments, the substance comprises fabric, metal, or plastic. In some embodiments of the method, protecting involves lubricating the substance where the substance is metal. Such a method is exemplified by the protecting applications listed for dry cleaning fluids, industrial solvents, crop protection solvents/coating oils, grain de-dusting oils, metal working fluids, industrial cleaning fluids, lubricating base oils, polymerization fluids, transformer oils, cosmetic oils, food preparation oils, and drilling fluids and hydraulic fracturing fluids of the present technology.

Dry Cleaning Fluids:

Bio-based synthetic fluids of this technology may be used as a substitute for petroleum-based solvents and perchloroethylene for dry cleaning of apparel. These fluids comprise hydrocarbons in the C₁₀-C₁₅ range. The paraffinic nature of the fluid (specifically its non-corrosive, non-polar properties) allows it to be used with many sensitive fabrics. They remove oil and grease effectively, aid in removing water-soluble dirt when combined with effective detergents, and are virtually odorless. The kinematic viscosities of these fluids are less than 10 cSt at 40° C. For reducing risk of fire, the flash point is generally above 38° C. Dry cleaning fluids of this technology include hydrocarbons in the C₁₀-C₁₅ range.

Industrial Solvents:

Bio-based synthetic fluids of this technology may be used as solvents for paints, inks, adhesives, and coatings. These fluids comprise paraffinic hydrocarbons in the C₅-C₂₀ range. Due to virtual absence of aromatic hydrocarbons and odors, these fluids meet increasingly stringent regulatory requirements. The bio-based synthetic fluids are characterized by selective solvency as characterized by an aniline number greater than about 80° C., and a Kauri-Butanol value greater than about 19. They are an effective substitute for petroleum-based solvents, including ISOPAR® and SOLTROL® products. (ISOPAR® and SOLTROL® are trademarks of ExxonMobil Chemical and Chevron Phillips Chemical respectively.) The viscosities of these fluids are less than about 10 cSt at 40° C., with volatility (flash point and distillation/boiling range) adjusted according to the specific application. As such, the lighter hydrocarbons, such as those in the C₅-C₇ range, may be stripped/distilled in order to provide industrial solvents having higher flash points and thus with a reduced risk of fire.

Crop protection Solvents/Coating Oils:

Bio-based synthetic fluids of this technology may be used as agricultural solvents and spray oils. These fluids include paraffinic hydrocarbons in the C₅-C₂₀ range for solvent applications (e.g. for dissolving pesticides and herbicides), and in the C₁₆-C₃₆ range for coating oil applications. Examples of crop protection solvent applications include dissolving and spraying pesticides. These include applications where the solvent is used to extract a natural herbicide for crop protection. In these cases, selective solvency, as indicated by an aniline number greater than about 80° C., and a Kauri-Butanol value greater than about 19, is a key attribute of the paraffinic solvent.

When used as coating oil, the fluid is applied to the plant leaves forming a film that protects the plant from fungi and pests. Because the coating oil is a non-toxic chemical, as defined by an eco-toxicity where LC₅₀>3.5 mg/L (as described above), the pests cannot become immune to the product. The spray oil naturally bio-degrades and evaporates during the growth cycle of the plant. And because the bio-based fluids are naturally free-of sulfur, they do not leave a sulfonic residue. Typically, for coating oil applications, the fluid viscosity is greater than about 10 cSt at 40° C.

Grain De-Dusting Oil:

This application is similar to the crop protection coating oil. Bio-based synthetic fluids of the present technology that include hydrocarbons in the C₁₆-C₃₆ range provide the required performance, mitigating dust accumulation when handling grain. For this application, fluid viscosity is greater than about 10 cSt at 40° C.

Metal Working Fluids:

Bio-based synthetic fluids of this technology may be used as metal working fluids, including metal lubricating and metal rolling fluids. For applications such as aluminum rolling (e.g. for preparing rolls of aluminum foils) paraffinic hydrocarbons in the C₁₁-C₂₀ range, having kinematic viscosities less than about 10 cSt at 40° C. and flash points above about 60° C. are most suitable.

For applications involving more severe metal-metal contact where lubricating properties are desired, chlorinated paraffins from chlorination of the HDO product as described above, or bio-derived synthetic fluids of the present technology having a carbon number in the C₁₆-C₃₆ range and a kinematic viscosity greater than about 10 cSt at 40° C. are desired. These fluids cool and lubricate metal surfaces, reducing friction and tool wear while removing residual metallic pieces.

Industrial Cleaning Fluids:

Bio-based synthetic fluids of this technology are suitable substitutes for petroleum kerosene for use as industrial cleaners. Unlike the petroleum kerosene that can have up to 30% aromatic hydrocarbons, the bio-based synthetic fluids contain virtually no aromatics and are therefore low in toxicity and odor, and meet stringent regulatory requirements for occupational exposure.

Lubricating Base Oils:

Bio-based synthetic fluids of this technology, comprising oligomerized hydrocarbons, have kinematic viscosities greater than about 10 cSt at 40° C., preferably greater than about 20 cSt at 40° C., and viscosity index values (measure of viscosity stability within operating temperature range) suitable for lube base oil applications.

Polymerization Fluids:

Bio-based synthetic fluids of this technology may be used for various solution and slurry polymerization processes such as the linear low density polyethylene process. Additionally, these fluids may be used for foam blowing processes, as an environmentally friendly substitute for chlorinated hydrocarbons. Examples of such foam blowing processes include production of foamed polystyrene (e.g. STYROFOAM®) and foamed polyurethane. Isoparaffinic hydrocarbons (e.g. HDO hydroisomerization products) in the C₅-C₉ range are particularly well-suited for these applications.

Transformer Oils:

Bio-based synthetic fluids of this technology are suitable for use as transformer fluids due to their low dielectric constants (from about 2 to about 3 at in the range from about 50° C. to about 200° C.) and very low water solubility. Oligomerized bio-based fluids having carbon numbers in the C₂₀-C₃₆ range are preferred due to their very high flash points.

Cosmetic Oils:

Bio-based synthetic fluids of this technology may be used as ingredients in baby lotions, cold creams, ointments and cosmetics. The odorless, tasteless, and inherently non-toxic attributes of these fluids make them attractive for these applications. The fluids of this technology in the C₁₆-C₃₆ range having a kinematic viscosity greater than about 10 cSt at 40 C are particularly well-suited for use in cosmetics.

Food Preparation Oils:

Bio-based synthetic fluids of this technology may be used for food contact applications. Due to their properties in preventing water absorption, and with their inherent non-toxicity and low odor, these bio-based synthetic fluids may be used to preserve wooden cutting boards, salad bowls and other wooden kitchenware/utensils. Rubbing small amounts of the oils on the wooden kitchenware fills cracks therein and prevents water/food accumulation which can lead to formation of bacteria in addition to degradation of the wooden article.

Drilling Fluids and Hydraulic Fracturing Fluids:

Bio-based synthetic fluids of this technology may be used as base fluids for drilling mud applications, including for offshore applications where a good balance of thermal stability, eco-toxicity and bio-degradability is desired.

In an aspect, a method is provided which involves producing an orifice in a substrate by at least injecting a paraffinic fluid into the substrate, wherein the paraffinic fluid comprises a hydrodeoxygenated product; the hydrodeoxygenated product is produced by hydrodeoxygenating a bio-derived feed; the bio-derived feed comprising bio-derived fatty acids, fatty acid esters, or a combination thereof; the hydrodeoxygenated product comprises n-paraffins; the paraffinic fluid contains less than about 1 wt % aromatics; and the n-paraffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms. The paraffinic fluid may be any one of the compositions provided by the present technology, including, but not lmited to, the oligermized product, the chlorinated product, the olefinic fluid, the HDO product, the hydroisomerized product, or mixtures of any two or more thereof. As described above, the paraffinic fluids of the present technology have flash points, thermal stabilities, viscosities, eco-toxicities and biodegradabilities excellently suited for such a method. In some embodiments, the hydrodeoxygenated product includes n-paraffins in the range of about 80 wt % to about 100 wt %; cycloparaffins in the range of about 0 wt % to about 10 wt %; and less than about 1 wt % total aromatics. In some embodiments, the paraffinic fluid further includes a hydroisomerized product produced by at least partially hydroisomerizing the hydrodeoxygenated product; wherein the hydroisomerized product comprises isoparaffins where at least about 80 wt % of the isoparaffins are mono-methyl branched paraffins; the mono-methyl branched paraffins comprise less than about 30 wt % terminal branched isoparaffins; and the isoparaffins have a kinematic viscosity of less than about 10 cSt at 40° C. and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms.

In some embodiments, the paraffinic fluid has a kinematic viscosity less than about 10 cSt at 40° C. In such embodiments, the paraffinic fluid may have a kinematic viscosity at 40° C. of about 9 cSt, about 8 cSt, about 7 cSt, about 6 cSt, about 5 cSt, about 4 cSt, about 3 cSt, about 2 cSt, about 1 cSt, and ranges in between any two of these values or below any one of these values. In some embodiments, the paraffinic fluid has a kinematic viscosity greater than about 10 cSt at 40° C. In such embodiments, the paraffinic fluid may have a kinematic viscosity at 40° C. of about 12 cSt, about 14 cSt, about 16 cSt, about 18 cSt, about 20 cSt, about 22 cSt, about 24 cSt, about 26 cSt, about 28 cSt, about 30 cSt, and ranges in between any two of these values or greater than any one of these values. In some embodiments, the paraffinic fluid has a kinematic viscosity greater than about 20 cSt at 40° C.

In some embodiments, the substrate comprises a soil substrate, a topsoil substrate, a subsoil substrate, a clay substrate, a sand substrate, a rock substrate, or a stone substrate. In some embodiments, the bio-derived fatty acids, fatty acid esters, or a combination thereof comprises algae oils, beef tallow, camelina oil, canola oil, rapeseed oil, castor oil, choice white grease, coconut oil, coffee bean oil, corn oil, cottonseed oil, fish oils, hemp oil, Jatropha oil, linseed oil, mustard oil, palm oil, palm kernel oil, poultry fat, soybean oil, sunflower oil, tall oil, tall oil fatty acid, Tung oil, used cooking oils, yellow grease, products of the food industry, or combinations of any two or more thereof. In some embodiments, the bio-derived fatty acids, fatty acid esters, or a combination thereof comprise soybean oil, corn oil, cottonseed oil, canola oil, coconut oil, sunflower oil, palm oil, palm kernel oil, rapeseed oil, or a combination of any two or more thereof. In some embodiments, the step of producing an orifice comprises hydraulic fracturing of the substrate with the paraffinic fluid.

Integrated Process for Production of Bio-Based Industrial Fluids:

An embodiment of the inventive method for producing bio-based industrial fluids is presented in FIG. 1. Referring to FIG. 1, a bio-based feed 102 comprising fatty acids and/or fatty acid esters is combined with a compressed treat gas 104 to form reactor feed stream 106 and achieve hydrodeoxygenation (HDO) in HDO unit 110. The bio-based feed 102 comprises any one or more of the oils, fats, or greases recited earlier herein in this application. The bio-based feed 102 and treat gas 104 are pumped and compressed respectively to a pressure within the range described earlier herein.

The treat gas 104 for the HDO reaction is a hydrogen-rich gas, with a hydrogen concentration in the range of about 70 mol % to about 100 mol %. In some embodiments, the hydrogen concentration is between about 82 mol % and about 99 mol %. The main impurities present in the treat gas 104 include methane, ethane, propane, n-/iso-butane, hydrogen sulfide, carbon monoxide, carbon dioxide, ammonia, and water.

The HDO unit 110 comprises a preheater to raise the temperature of reactor feed 106 to achieve HDO reactor operation within the temperature range described previously in the application. In addition to the preheater, the HDO unit 110 includes an HDO reactor, separator drums/vessels, and a product stripper. The drums/vessels separate a water byproduct 112 and an HDO gas 114 from HDO product 116. The product stripper is employed for removal of residual byproduct ammonia, hydrogen sulfide, and carbon oxides, dissolved in the HDO product 116. The HDO product 116 is a paraffinic hydrocarbon composition comprising n-paraffins in the C₁₅-C₁₈ range, with elemental sulfur and elemental nitrogen less than about 5 wppm and elemental oxygen less than about 0.1 wt %. In some embodiments, elemental sulfur and elemental nitrogen are less than 1 wppm in the paraffinic hydrocarbon composition. In some embodiments, the HDO product 116 is partially recycled to the HDO reactor as a solvent/diluent for bio-based feed 102.

The HDO gas 114, containing same byproducts in addition to light hydrocarbons such as methane and propane, is optionally subjected to treatment (e.g. scrubbing with a solvent, water, or caustic/amine solutions) to reduce the concentration of these molecules in the gas 114. In some embodiments, the gas 114 is partially recycled to the HDO reactor.

The HDO product 116 is combined with treat gas 118 to form a hydroisomerization unit feed 119. The treat gas is a hydrogen-rich gas stream having the specifications of treat gas 104, but preferably containing less than about 10 ppm hydrogen sulfide, ammonia, or carbon monoxide. If needed, the HDO product 116 and treat gas 118 are pressurized/compressed to a value within the hydroisomerization operating pressure range specified earlier in this application.

The hydroisomerization unit 120 comprises a feed preheater, a hydroisomerization reactor, and separation drums for separating the hydroisomerization product 124 from the hydroisomerization gas 122. The hydroisomerization gas 122 may contain light hydrocarbons formed in the hydroisomerization reactor via hydrocracking side reactions therein.

The preheater in the hydroisomerization unit 120 raises the temperature of the feed for operating the hydroisomerization reactor within the temperature range indicated earlier in this application.

The hydroisomerization gas 122 is combined with the treat gas 104 and/or the treat gas 118, via a compression stage if desired.

The hydroisomerization product 124, comprising paraffinic hydrocarbons in the C₅-C₁₈ range, is directed to oligomerization unit 130, where it is combined with an organic peroxide initiator 126 according to conditions and limitations provided previously. In embodiments where a batch oligomerization reactor is employed, the oligomerization unit 130 is equipped with a plurality of feed tanks. In these embodiments, one tank is used to charge the oligomerization reactor while the other is being filled with hydroisomerization product 124. The oligomerization effluent 132 includes both oligomerized and unconverted components of hydroisomerization product 124. As such, the oligomerization effluent 132 is a paraffinic hydrocarbon composition in the C₅-C₃₇+ range, characterized by a high degree of C₂+ chain branching.

The oligomerization effluent is directed to a fractionation unit 140. The fractionation unit may be one distillation column with side draws, or a plurality of columns operating at different pressures. Therein the oligomerization effluent is fractionated into Fraction 142 comprising hydrocarbons in the C₅-C₁₅ range, Fraction 144 comprising hydrocarbons in the C₁₆-C₁₈ range, and Fraction 146 comprising hydrocarbons in the C₁₉-C₃₇+ range. Fraction 144 may be used for solvents, drilling fluids, hydraulic fracturing fluids, and other industrial fluid applications where kinematic viscosity values are less than about 10 cSt at 40° C. Fraction 146 may be used for lubricating oils, dielectric fluids, grain de-dusting fluids, mineral oil, and other applications where the kinematic viscosity is greater than about 10 cSt at 40 C. In some embodiments, it is necessary to further fractionate the fluid fraction comprising C₃₇+ fractions in order to meet the maximum boiling temperature specified for the fluid.

Fraction 142 may be partially or completely recycled to oligomerization unit 130. Alternatively, Fraction 142 may be further fractionated into a C₅-C₉ ranged and C₁₀-C₁₅ ranged fractions for use as other solvents or fuels. The fluid fractions are preferably additized with an anti-oxidant, and other additives specific to the application, before drumming and shipping. The anti-oxidant is preferably a hindered phenol introduced at a concentration between about 2 and about 200 wppm. In some embodiments, the anti-oxidant is at a concentration between about 10 wppm and about 100 wppm.

The present invention, thus generally described, will be understood more readily by reference to the following examples, which are provided by way of illustration and are not intended to be limiting of the present invention.

EXAMPLES Example 1 Demonstration of the Bio-Degradability of a Bio-Based Synthetic Hydrocarbon Fluids

Canola oil was hydrodeoxygenated in a 100 cc tubular reactor packed with 20 cc Mo catalyst (top layer) and 80 cc NiMo catalyst (bottom layer) and then pressurized to 1600 psig with hydrogen. The catalysts were commercially available products obtained in oxide form. The catalysts were sulfided in the reactor using dimethyl disulfide (DMDS), following a ramp-hold temperature profile. The first hold was 12 hrs at 400° F. (wherein H₂5 breakthrough was confirmed), and the second hold was about 10 hrs at 700° F. The temperatures were lowered to about 450° F. before introduction of 100% canola oil (spiked with 100 ppm sulfur as DMDS). After a break-in period of partial hydrodeoxygenation, the reactor temperature was raised to 640 F. The liquid hourly space velocity of canola oil was maintained at 1 vol/vol/hr, along with a 10,000 SCF/Bbl gas-to-oil ratio.

The canola oil feed and HDO product were both analyzed for elemental oxygen. The feed was 11.1 wt % oxygen whereas the HDO product was below detection limit (<0.1 wt % oxygen). The HDO product had a flash point of 138° C., a viscosity of 3.68 cSt at 40° C., and density of 0.800 kg/L.

The HDO product was subjected to biodegradability test according to ASTM D5864-05. After 23 days of exposure to microorganisms at the conditions specified in the test method, with room temperature in the 20-25° C. range, the paraffinic HDO product degradation as measured by CO₂ production was found to be 44.2%. By comparison, the biodegradability of poly alpha olefins is reported to be in the 0-25% range.

Example 2 Hydroisomerized HDO Product Fractions

HDO paraffins were hydroisomerized (HI) according to the conditions described in this technology, using a Pt/Pd-on-amorphous silica/alumina catalyst. The hydroisomerized products were fractionated into different cuts using both laboratory as well as commercial scale distillation columns. The fractionation cuts' boiling ranges corresponded to commercial grades of petroleum-based paraffinic fluids such as ISOPAR® L, ISOPAR® M, ISOPAR® V, SOLTROL® 170, and SOLTROL® 220. The results are summarized in Table 1.

TABLE 1 Comparison of Bio-Based Isoparaffin Fluid Fractions (HI Cuts) to Commercial Petro-Solvents ISOPAR GRADE L M V ISOPAR and Equivalent Products ISOPAR HI Cut 2 ISOPAR SOL-170 HI Cut 3 ISOPAR SOL-220 HI Cut 4 HI BTMS Solvency Kauri-butanol value, ASTM D1133 27 25 25 24.6 23 23 NA³ 20.5 19 Aniline Point (° C.) 85 80 91 91 86 92 NA 94 98 Volatility Flash Point, ASTM D56 (° C.) 64 60 93 87 87 129 100 121 124 Distillation, ASTM D86 IBP (° C.) 189 165 223 ≧216 198 273 ≧218 228 273 Distillation, ASTM D86 EP (° C.) 207 209 254 ≦246 243 312 ≦315 281 304 Specific Gravity @ 15.6 C., ASTM D1250 0.77 0.77 0.79 0.78 0.77 0.83 NA 0.78 0.784 Composition, wt % Saturates 99.9 >99 99.9 >99 99.8 NA >99 99.7 Aromatics <0.01 <1 <0.05 0.01 <1 <0.5 NA <1 0.3 Notes: 1. ISOPAR is a trademark of ExxonMobil Chemical 2. SOLTROL (“SOL”) is a trademark of Chevron Phillips Chemical ³NA = Data not available

As observed in Table 1, the bio-based fluids, HI Cuts 2-4 and HI Btms, have the desired selective solvency for use as industrial solvents: Kauri-Butanol values greater than about 19, and aniline points greater than about 80° C.

The HI Btms fraction was further analyzed for comparison with two commercial petroleum-based drilling fluids, recognized for their relatively low ecotoxicity, high flash points, and low pour points. These products are offered for offshore applications. Table 2 provides a summary of the results.

TABLE 2 Comparison of Bio-Based Isoparaffinic Fluid (HI Btms) to Commercial Petro-Based Drilling Fluids Property CLAIRSOL NS^((a)) ESCAID 120^((b)) HI Btms Specific Gravity 0.82 0.818 0.784 Flash Point, ° C. 122 101 124 Pour Point, ° C. −18 −24 <−12 Aromatics, wt % <0.5 0.9 <0.5 Viscosity at 20° C., cSt Viscosity at 40° C., cSt 3.4 2.36 3.49 Aniline Pt., ° C. 84 98 Distillation, ° C. IBP 261 235 273 FBP 293 270 304 Notes: ^((a))CLAIRSOL is tradename of Petrochem Carless, a leading supplier of drilling base fluids in Europe ^((b))ESCAID is tradename of ExxonMobil Chemical, a leading supplier of drilling base fluids

The table shows that the bio-based drilling fluid (or drilling mud base fluid) meets all the performance parameters presently provided by the petroleum-based drilling fluids.

Example 3 Peroxide-Initiated Oligomerization of Paraffins

100 parts by weight of a hydroisomerized HDO product is introduced to a round-bottom flask reactor equipped with a mechanical stirrer, a reflux condenser, a temperature indicator, and a heating mantle. The hydroisomerized HDO product is analyzed via gas chromatography (GC) and is found to consist mainly of C₉-C₁₈ n-paraffins and iso-paraffins. Upon reaching about 200° C., 20 parts by weight of LUPEROX 101 organic peroxide [2,5-dimethyl 2,5-di(t-butylperoxy)hexane; purchasable from Aldrich] is added in 10 equal parts over 5 hours. Upon reaching the 6^(th) hour, the reactor is cooled and analyzed via GC where increase in carbon number is confirmed. The product is distilled to remove the lighter, un-reacted components and the byproducts of peroxide decomposition. The higher carbon number product is then tested for biodegradability according to D5864 guidelines and expected to display at least 40+% biodegradation after 23 days of exposure to micro-organisms.

While certain embodiments have been illustrated and described, it should be understood that changes and modifications can be made therein in accordance with ordinary skill in the art without departing from the technology in its broader aspects as defined in the following claims.

The embodiments, illustratively described herein may suitably be practiced in the absence of any element or elements, limitation or limitations, not specifically disclosed herein. Thus, for example, the terms “comprising,” “including,” “containing,” etc. shall be read expansively and without limitation. Additionally, the terms and expressions employed herein have been used as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the claimed technology. Additionally, the phrase “consisting essentially of” will be understood to include those elements specifically recited and those additional elements that do not materially affect the basic and novel characteristics of the claimed technology. The phrase “consisting of” excludes any element not specified.

The present disclosure is not to be limited in terms of the particular embodiments described in this application. Many modifications and variations can be made without departing from its spirit and scope, as will be apparent to those skilled in the art. Functionally equivalent methods and compositions within the scope of the disclosure, in addition to those enumerated herein, will be apparent to those skilled in the art from the foregoing descriptions. Such modifications and variations are intended to fall within the scope of the appended claims. The present disclosure is to be limited only by the terms of the appended claims, along with the full scope of equivalents to which such claims are entitled. It is to be understood that this disclosure is not limited to particular methods, reagents, compounds compositions or biological systems, which can of course vary. It is also to be understood that the terminology used herein is for the purpose of describing particular embodiments only, and is not intended to be limiting.

In addition, where features or aspects of the disclosure are described in terms of Markush groups, those skilled in the art will recognize that the disclosure is also thereby described in terms of any individual member or subgroup of members of the Markush group.

As will be understood by one skilled in the art, for any and all purposes, particularly in terms of providing a written description, all ranges disclosed herein also encompass any and all possible subranges and combinations of subranges thereof. Any listed range can be easily recognized as sufficiently describing and enabling the same range being broken down into at least equal halves, thirds, quarters, fifths, tenths, etc. As a non-limiting example, each range discussed herein can be readily broken down into a lower third, middle third and upper third, etc. As will also be understood by one skilled in the art all language such as “up to,” “at least,” “greater than,” “less than,” and the like, include the number recited and refer to ranges which can be subsequently broken down into subranges as discussed above. Finally, as will be understood by one skilled in the art, a range includes each individual member.

All publications, patent applications, issued patents, and other documents referred to in this specification are herein incorporated by reference as if each individual publication, patent application, issued patent, or other document was specifically and individually indicated to be incorporated by reference in its entirety. Definitions that are contained in text incorporated by reference are excluded to the extent that they contradict definitions in this disclosure.

Other embodiments are set forth in the following claims. 

What is claimed is:
 1. A method comprising altering the viscosity of bio-derived paraffins to produce a paraffinic fluid, wherein the altering step comprises chlorinating the bio-derived paraffins to produce a chlorinated product, where the chlorinated product comprises haloalkanes and has a kinematic viscosity of greater than about 10 cSt at 40° C.; the paraffinic fluid comprises the chlorinated product; the bio-derived paraffins comprise a hydrodeoxygenated product produced by hydrodeoxygenating a bio-based feed where the bio-based feed comprises bio-derived fatty acids, fatty acid esters, or a combination thereof; and the bio-derived paraffins comprise n-paraffins where the n-paraffins have a kinematic viscosity of less than about 10 cSt at 40° C.; and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms.
 2. The method of claim 1, wherein chlorinating the bio-derived paraffins comprises contacting the bio-derived paraffins with chlorine gas at a temperature between about 60° C. and about 150° C. to produce the chlorinated product.
 3. The method of claim 2, wherein the chlorinated product is about 30 wt % to about 70 wt % chlorine.
 4. The method of claim 2, wherein the chlorinated product has less than about 1 wt % aromatics.
 5. The method of claim 2, wherein the chlorinated product is free of benzene.
 6. The method of claim 2, wherein the hydrodeoxygenated product has less than about 1 wt % aromatics; the chlorinated product has less than about 1 wt % aromatics; and the paraffinic fluid has less than about 1 wt % aromatics.
 7. The method of claim 2, wherein the hydrodeoxygenated product has less than about 0.1 wt % aromatics; the chlorinated product has less than about 0.1 wt % aromatics; and the paraffinic fluid has less than about 0.1 wt % aromatics.
 8. The method of claim 2, wherein the temperature for contacting the bio-derived paraffins with chlorine gas is about 80° C. to about 120° C.
 9. The method of claim 2, wherein contacting the bio-derived paraffins with chlorine gas does not involve a catalyst.
 10. The method of claim 2, wherein contacting the bio-derived paraffins with chlorine gas further comprises UV light.
 11. The method of claim 2, further comprising purging the chlorinated product with air or nitrogen.
 12. The method of claim 2, wherein the paraffinic fluid comprises bio-derived paraffins within the C₁₆-C₃₆ range.
 13. The method of claim 1, wherein the bio-derived paraffins are produced by at least partially hydroisomerizing the hydrodeoxygenated product to produce a hydroisomerized product; wherein the bio-derived paraffins comprise the hydrodeoxygenated product and the hydroisomerized product; the hydrodeoxygenated product comprises n-paraffins; the hydroisomerized product comprises isoparaffins where at least about 80 wt % of the isoparaffins are mono-methyl branched paraffins and the mono-methyl branched paraffins comprise less than about 30 wt % terminal branched isoparaffins; and the isoparaffins have a kinematic viscosity of greater than about 10 cSt at 40° C.; and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms.
 14. The method of claim 13, wherein the hydrodeoxygenated product comprises n-paraffins in the range of about 80 wt % to about 100 wt %; cycloparaffins in the range of about 0 wt % to about 10 wt %; and less than about 1 wt % total aromatics.
 15. The method of claim 13, wherein the hydrodeoxygenated product comprises n-paraffins in the range of about 90 wt % to about 100 wt %; cycloparaffins in the range of about 0 wt % to about 10 wt %; and less than about 0.1 wt % total aromatics.
 16. The method of claim 2, wherein the bio-derived paraffins are produced by hydrodeoxygenating the bio-based feed to produce a hydrodeoxygenated product; and at least partially hydroisomerizing the hydrodeoxygenated product to produce a hydroisomerized product; wherein the bio-derived paraffins comprise the hydrodeoxygenated product and the hydroisomerized product; the hydrodeoxygenated product comprises n-paraffins; the hydroisomerized product comprises isoparaffins where at least about 80 wt % of the isoparaffins are mono-methyl branched paraffins and the mono-methyl branched paraffins comprise less than about 30 wt % terminal branched isoparaffins; and the isoparaffins have a kinematic viscosity of greater than about 10 cSt at 40° C.; and have a biodegradability of at least about 40% after about 23 days of exposure to microorganisms.
 17. The method of claim 16, wherein contacting the bio-derived paraffins with chlorine gas does not involve a catalyst.
 18. The method of claim 16, wherein contacting the bio-derived paraffins with chlorine gas further comprises UV light.
 19. The method of claim 16, further comprising purging the chlorinated product with air or nitrogen.
 20. The method of claim 16, wherein paraffinic fluid comprises bio-derived paraffins within the C₁₆-C₃₆ range.
 21. The method of claim 16, wherein the hydrodeoxygenated product comprises n-paraffins in the range of about 80 wt % to about 100 wt %; cycloparaffins in the range of about 0 wt % to about 10 wt %; and less than about 1 wt % total aromatics.
 22. The method of claim 16, wherein the hydrodeoxygenated product comprises n-paraffins in the range of about 90 wt % to about 100 wt %; cycloparaffins in the range of about 0 wt % to about 10 wt %; and less than about 0.1 wt % total aromatics.
 23. The method of claim 1, wherein the bio-derived fatty acids, fatty acid esters, or a combination thereof comprises algae oils, beef tallow, camelina oil, canola oil, rapeseed oil, castor oil, choice white grease, coconut oil, coffee bean oil, corn oil, cottonseed oil, fish oils, hemp oil, Jatropha oil, linseed oil, mustard oil, palm oil, palm kernel oil, poultry fat, soybean oil, sunflower oil, tall oil, tall oil fatty acid, Tung oil, used cooking oils, yellow grease, products of the food industry, or combinations of any two or more thereof.
 24. The method of claim 1, wherein the bio-derived fatty acids, fatty acid esters, or a combination thereof comprise soybean oil, corn oil, cottonseed oil, canola oil, coconut oil, sunflower oil, palm oil, palm kernel oil, rapeseed oil, or a combination of any two or more thereof.
 25. The method of claim 1, wherein the paraffinic fluid is free of benzene.
 26. The paraffinic fluid produced by the method of claim
 1. 27. The paraffinic fluid of claim 26, wherein the paraffinic fluid is used as a protecting agent, a cleaning agent, or a combination of both.
 28. The paraffinic fluid of claim 26, wherein the paraffinic fluid acts as a flame retardant. 